Catalyst composition, the method of manufacturing, and the process of use thereof in aromatics alkylation

ABSTRACT

A catalyst composition comprises a crystalline MCM-22 family molecular sieve and a binder, wherein the catalyst composition is characterized by an extra-molecular sieve porosity greater than or equal to 0.122 ml/g for pores having a pore diameter ranging from about 2 nm to about 8 nm, wherein the porosity is measured by N 2  porosimetry. The catalyst composition may be used for the process of alkylation or transalkylation of an alkylatable aromatic compound with an alkylating agent. The molecular sieve may have a Constraint Index of less than 12, e.g., less than 2. Examples of molecular sieve useful for this disclosure are a MCM-22 family molecular sieve, zeolite Y, and zeolite Beta.

PRIORITY CLAIM

This application is a divisional of and claims priority to U.S. patentapplication Ser. No. 11/643,530, filed 21 Dec. 2006, now U.S. Pat. No.7,919,421, the disclosure of which is herein incorporated by referencein its entirety.

FIELD

This invention relates to a novel catalyst composition, the method ofmanufacturing, and the process of using thereof for hydrocarbonconversions. In particular, the novel catalyst composition of thisdisclosure comprises a crystalline MCM-22 family molecular sieve and abinder, wherein the catalyst composition is characterized by acumulative extra-molecular sieve pore volume greater than or equal to0.122 ml/g for pores having a pore diameter ranging from about 2 nm toabout 8 nm. The hydrocarbon conversions comprise alkylation and/ortransalkylation of alkylatable aromatics.

BACKGROUND OF THIS DISCLOSURE

The alkylation of aromatic hydrocarbon compounds employing zeolitecatalysts is known and understood in the art. U.S. Pat. No. 5,334,795describes the liquid phase alkylation of benzene with ethylene in thepresence of MCM-22 to produce ethylbenzene; and U.S. Pat. No. 4,891,458discloses liquid phase alkylation and transalkylation processes usingzeolite beta.

Zeolite-based catalysts are used in the alkylation of benzene withpropylene to produce cumene. U.S. Pat. No. 4,992,606 discloses a processfor preparing cumene using MCM-22 in liquid phase.

The alkylation of benzene with ethylene and propylene to formethylbenzene (EB) and cumene respectively produce the desiredmonoalkylated compound along with undesired polyalkylated impurities bycontacting an alkylatable aromatic compound and an alkylating agent inthe presence of a catalyst. Therefore, there is a need for novelcatalyst composition and the process of using such catalyst compositionin the alkylation and/or transalkylation processes that increase theselectivity to the desired monoalkylated aromatic compound at equivalentactivity. This disclosure meets this and other needs.

SUMMARY OF THIS DISCLOSURE

In some embodiments, this disclosure relates to a catalyst compositioncomprising:

-   -   (a) a crystalline MCM-22 family molecular sieve; and    -   (b) a binder,        wherein the catalyst composition is characterized by a        cumulative extra-molecular sieve pore volume greater than or        equal to 0.122 ml/g, preferably greater than or equal to 0.125        ml/g, more preferably greater than or equal to 0.13 ml/g, for        pores having a pore diameter ranging from about 2 nm to about 8        nm, wherein the pore volume is measured by N₂ porosimetry.

In one aspect, the extra-molecular sieve porosity is less than or equalto 5 ml/g.

In some embodiments, the catalyst composition further comprises a secondmolecular sieve having a Constraint Index of less than 12. In anotherembodiment the catalyst composition further comprises a second molecularsieve having a Constraint Index of less than 2. In one preferredembodiment, the second molecular sieve has a framework type of at leastone of FAU, *BEA, MFI, MTW, and any combination thereof. In anotherpreferred embodiment, the crystalline MCM-22 family molecular sievecomprises at least one of MCM-22, MCM-36, MCM-49, MCM-56, ITQ-1, ITQ-30,and any combination thereof.

In one aspect, the binder comprises at least one compound of Group 1 toGroup 17 element, preferably the binder comprises titanium compound,alumina compound, silicon compound, or any mixture thereof, morepreferably the binder is selected from a group consisting of titaniumoxide, titanium hydroxide, titanium sulfate, titanium phosphate,aluminum oxide, aluminum hydroxide, aluminum sulfate, aluminumphosphate, silica, silicates, aluminosilicates, titanosilicates,titanoaluminosilicates, aluminophosphates, metallophosphates,metalloaluminophosphates, silicoaluminophosphates, and any combinationthereof.

In some embodiments, the catalyst composition of this disclosure has atleast 1 wt %, preferably at least 10 wt %, more preferably at least 50wt %, even more preferably at least 60 wt %, at least 65 wt %, at least70 wt %, at least 75 wt %, and most preferably at least 80 wt %, of thecrystalline MCM-22 family molecular sieve based on the total weight ofthe catalyst composition.

In other embodiments, this disclosure relates to a process foralkylation or transalkylation of an alkylatable aromatic compound withan alkylating agent to produce a monoalkylated aromatic compound,comprising the steps of:

-   -   contacting at least one the alkylatable aromatic compound and at        least one the alkylating agent with a catalyst composition of        this disclosure under suitable alkylation or transalkylation        conditions in at least one reaction zone, to produce at least        one effluent which comprises the monoalkylated aromatic compound        and a monoalkylated aromatic compound selectivity;        wherein the monoalkylated aromatic compound selectivity of the        catalyst composition of this disclosure is greater than the        monoalkylated aromatic compound selectivity of a catalyst        composition having an extra-molecular sieve porosity outside the        extra-molecular sieve porosity range of the catalyst composition        of this disclosure for pores having a pore diameter ranging from        about 2 nm to about 8 nm, when the reaction zone is operated        under equivalent alkylation or transalkylation conditions.

In one aspect, the suitable alkylation or transalkylation conditionsinclude a temperature from about 100° C. to about 400° C., a pressurefrom about 20.3 to 4500 kPa-a, a WHSV from about 0.1 to about 10 hr⁻¹,and a molar ratio of the alkylatable compound over the alkylating agentfrom about 0.1:1 to 50:1.

In a preferred embodiment, the monoalkylated aromatic compound comprisesethylbenzene, the alkylatable aromatic compound comprises benzene, andthe alkylating agent comprises ethylene. In another preferredembodiment, the monoalkylated aromatic compound comprises cumene, thealkylatable aromatic compound comprises benzene, and the alkylatingagent comprises propylene.

In yet other embodiments, this disclosure relates to a process forpreparing the catalyst composition of this disclosure comprising thesteps of:

-   -   (a) providing a crystalline MCM-22 family molecular sieve and a        binder to form a mixture; and    -   (b) forming the mixture into the catalyst composition.        wherein the catalyst composition is characterized by a        cumulative extra-molecular sieve pore volume greater than or        equal to 0.122 ml/g, preferably greater than or equal to 0.125        ml/g, more preferably greater than or equal to 0.13 ml/g, for        pores having a pore diameter ranging from about 2 nm to about 8        nm, wherein the pore volume is measured by N₂ porosimetry.

In one embodiment, the forming step comprises extruding. In anotherembodiment, the catalyst composition has a shape of quadrulobe. In apreferred embodiment, the catalyst composition has at least 65 wt % ofcrystalline MCM-22 family molecular sieve based on the total weight ofthe catalyst composition. In yet another preferred embodiment, thecatalyst composition further at least 5 wt % of a molecular sieve havinga *BEA framework type based on the total weight of the catalystcomposition.

DETAILED DESCRIPTION OF THIS DISCLOSURE

Introduction

All patents, patent applications, test procedures, priority documents,articles, publications, manuals, and other documents cited herein arefully incorporated by reference to the extent such disclosure is notinconsistent with the present invention and for all jurisdictions inwhich such incorporation is permitted.

When numerical lower limits and numerical upper limits are listedherein, ranges from any lower limit to any upper limit are contemplated.

As used in this specification, the term “framework type” is used in thesense described in the “Atlas of Zeolite Framework Types,” 2001.

As used herein, the numbering scheme for the Periodic Table Groups isused as in Chemical and Engineering News, 63(5), 27 (1985).

The term “MCM-22 family material” (or “material of the MCM-22 family” or“molecular sieve of the MCM-22 family”), as used herein, includes:

-   (i) molecular sieves made from a common first degree crystalline    building block “unit cell having the MWW framework topology”. A unit    cell is a spatial arrangement of atoms which is tiled in    three-dimensional space to describe the crystal as described in the    “Atlas of Zeolite Framework Types”, Fifth edition, 2001, the entire    content of which is incorporated as reference;-   (ii) molecular sieves made from a common second degree building    block, a 2-dimensional tiling of such MWW framework type unit cells,    forming a “monolayer of one unit cell thickness”, preferably one    c-unit cell thickness;-   (iii) molecular sieves made from common second degree building    blocks, “layers of one or more than one unit cell thickness”,    wherein the layer of more than one unit cell thickness is made from    stacking, packing, or binding at least two monolayers of one unit    cell thick of unit cells having the MWW framework topology. The    stacking of such second degree building blocks can be in a regular    fashion, an irregular fashion, a random fashion, and any combination    thereof; or-   (iv) molecular sieves made by any regular or random 2-dimensional or    3-dimensional combination of unit cells having the MWW framework    topology.

The MCM-22 family materials are characterized by having an X-raydiffraction pattern including d-spacing maxima at 12.4±0.25, 3.57±0.07and 3.42±0.07 Angstroms (either calcined or as-synthesized). The MCM-22family materials may also be characterized by having an X-raydiffraction pattern including d-spacing maxima at 12.4±0.25, 6.9±0.15,3.57±0.07 and 3.42±0.07 Angstroms (either calcined or as-synthesized).The X-ray diffraction data used to characterize the molecular sieve areobtained by standard techniques using the K-alpha doublet of copper asthe incident radiation and a diffractometer equipped with ascintillation counter and associated computer as the collection system.Materials belong to the MCM-22 family include MCM-22 (described in U.S.Pat. No. 4,954,325), PSH-3 (described in U.S. Pat. No. 4,439,409),SSZ-25 (described in U.S. Pat. No. 4,826,667), ERB-1 (described inEuropean Patent No. 0293032), ITQ-1 (described in U.S. Pat. No.6,077,498), ITQ-2 (described in International Patent Publication No.WO97/17290), ITQ-30 (described in International Patent Publication No.WO2005118476), MCM-36 (described in U.S. Pat. No. 5,250,277), MCM-49(described in U.S. Pat. No. 5,236,575) and MCM-56 (described in U.S.Pat. No. 5,362,697). The entire contents of the patents are incorporatedherein by reference. U.S. Pat. Application Nos. 60/773,198, 60/773,014,60/834,030, 60/834,001, 60/834,032, 60/834,031, 60/834,115, and60/834,010 disclose members of the MCM-22 family materials.

It is to be appreciated the MCM-22 family molecular sieves describedabove are distinguished from conventional large pore zeolite alkylationcatalysts, such as mordenite, in that the MCM-22 materials have 12-ringsurface pockets which do not communicate with the 10-ring internal poresystem of the molecular sieve.

The zeolitic materials designated by the IZA-SC as being of the MWWtopology are multi-layered materials which have two pore systems arisingfrom the presence of both 10 and 12 membered rings. The Atlas of ZeoliteFramework Types classes five differently named materials as having thissame topology: MCM-22, ERB-1, ITQ-1, PSH-3, and SSZ-25.

The MCM-22 family molecular sieves have been found to be useful in avariety of hydrocarbon conversion processes. Examples of MCM-22 familymolecular sieve are MCM-22, MCM-49, MCM-56, ITQ-1, PSH-3, SSZ-25, andERB-1. Such molecular sieves are useful for alkylation of aromaticcompounds. For example, U.S. Pat. No. 6,936,744 discloses a process forproducing a monoalkylated aromatic compound, particularly cumene,comprising the step of contacting a polyalkylated aromatic compound withan alkylatable aromatic compound under at least partial liquid phaseconditions and in the presence of a transalkylation catalyst to producethe monoalkylated aromatic compound, wherein the transalkylationcatalyst comprises a mixture of at least two different crystallinemolecular sieves, wherein each of the molecular sieves is selected fromzeolite beta, zeolite Y, mordenite and a material having an X-raydiffraction pattern including d-spacing maxima at 12.4±0.25, 6.9±0.15,3.57±0.07 and 3.42±0.07 Angstroms.

As used herein, an “alkylatable aromatic compound” is a compound thatmay receive an alkyl group and an “alkylating agent” is a compound whichmay donate an alkyl group to an alkylatable aromatic compound. Oneexample of the alkylatable aromatic compounds is benzene. Examples ofthe alkylating agent are ethylene, propylene, polyalkylated aromaticcompound(s), e.g., di-ethylbenzene, tri-ethylbenzene,di-isopropylbenzene, and tri-isopropylbenzene

The term “wppm” as used herein is defined as parts per million byweight.

The term “aromatic” as used herein is to be understood in accordancewith its art-recognized scope which includes alkyl substituted andunsubstituted mono- and polynuclear compounds. Compounds of an aromaticcharacter, which possess a heteroatom, are also useful providedsufficient activity can be achieved if they act as catalyst poisonsunder the reaction conditions selected.

Catalyst

The catalyst composition of this disclosure comprises a crystallineMCM-22 family molecular sieve and a binder, wherein the catalystcomposition is characterized by a cumulative extra-molecular sieve porevolume greater than or equal to 0.122 ml/g, preferably greater than orequal to 0.125 ml/g, more preferably greater than or equal to 0.13 ml/g,for pores having a pore diameter ranging from about 2 nm to about 8 nm,wherein the pore volume is measured by N₂ porosimetry.

In some embodiments, the crystalline MCM-22 family molecular sieve ofthis disclosure comprises at least one of MCM-22, MCM-49, MCM-56, ITQ-1,ITQ-30, an intergrowth-phase thereof, or a mix phase thereof. In apreferred embodiment of this disclosure, the catalyst composition ofthis disclosure has at least 1 wt %, preferably at least 10 wt %, morepreferably at least 50 wt %, even more preferably at least 60 wt %, atleast 65 wt %, at least 70 wt %, at least 75 wt %, and most preferablyat least 80 wt %, of the crystalline MCM-22 family molecular sieve basedon the total weight of the catalyst composition. In yet anotherpreferred embodiment of this disclosure, the catalyst composition ofthis disclosure has at least 1 wt %, preferably at least 10 wt %, morepreferably at least 50 wt %, even more preferably at least 60 wt %, atleast 65 wt %, at least 70 wt %, at least 75 wt %, and most preferablyat least 80 wt %, of MCM-22, MCM-49, MCM-56, and/or any combinationthereof based on the total weight of the catalyst composition.

It will be understood by a person skilled in the art that thecrystalline MCM-22 family material may contain impurities, such asamorphous materials; unit cells having non-MWW framework topologies(e.g., MFI, MTW); and/or other impurities (e.g., heavy metals and/ororganic hydrocarbons). The crystalline MCM-22 family materials of thisdisclosure are preferably substantially free of non-MCM-22 familymaterial(s). The term “substantially free of non-MCM-22 familymaterial(s)” used herein means the crystalline MCM-22 family material ofthis disclosure preferably contains a minor proportion (less than 50 wt%), preferably less than 20 wt %, more preferably less than 10 wt %,even more preferably less than 5 wt %, and most preferably less than 1wt %, of non-MCM-22 family materials (“impurities”) in the crystallineMCM-22 family materials, which weight percent (wt %) values are based onthe combined weight of impurities and pure phase crystalline MCM-22family materials.

In some embodiments, the crystalline MCM-22 family molecular sieve ofthis disclosure may contain less than 10 weight percent, preferably lessthan 5 weight percent, even more preferably less than 1 weight percent,based on the total weight of the crystalline molecular sievecomposition, of non-MCM-22 family molecular sieve(s). Typical examplesof the non-MCM-22 family molecular sieve(s) co-existing with the MCM-22family molecular sieve(s) of this disclosure are Kenyaite, EU-1, ZSM-50,ZSM-12, ZSM-48, ZSM-5, Ferrierite, Mordenite, Solalite, and/or Analcine.Other examples of the non-MCM-22 family molecular sieve(s) co-existingwith the MCM-22 family molecular sieve(s) of this disclosure aremolecular sieves having framework type of EUO, MTW, FER, MOR, SOD, ANA,and/or MFI. The product of the synthesis may comprises less than 10weight percent, preferably less than 5 weight percent, even morepreferably less than 1 weight percent, based on the total weight of theproduct, of non-crystalline materials, e.g., quartz.

The MCM-22 crystalline material has a composition involving the molarrelationship:X₂O₃:(n)YO₂,wherein X is a trivalent element, such as aluminum, boron, iron and/orgallium, preferably aluminum, Y is a tetravalent element such as siliconand/or germanium, preferably silicon, and n is at least about 10,usually from about 10 to about 150, more usually from about 10 to about60, and even more usually from about 20 to about 40. In theas-synthesized form, the material has a formula, on an anhydrous basisand in terms of moles of oxides per n moles of YO₂, as follows:(0.005-1)M₂O:(1-4)R:X₂O₃:nYO₂wherein M is an alkali or alkaline earth metal, and R is an organicmoiety. The M and R components are associated with the material as aresult of their presence during synthesis, and are typically removed bypost-synthesis methods well known to those skilled in the art and/orhereinafter more particularly described.

To the extent desired, the original metal cations of the as-synthesizedmaterial can be replaced in accordance with techniques well known in theart, at least in part, by ion exchange with other cations. Preferredreplacing cations include metal ions, hydrogen ions, hydrogen precursor,e.g., ammonium, ions and mixtures thereof. Particularly preferredcations are those which tailor the catalytic activity for certainhydrocarbon conversion reactions. These include hydrogen, rare earthmetals and metals of Groups 1-17, preferably Groups 2-12 of the PeriodicTable of the Elements.

In some embodiments, the catalyst composition further comprises a secondmolecular sieve comprising at lease one of a medium pore molecular sievehaving a Constraint Index of 2-12 and/or a large pore molecular sievehaving a Constraint Index of less than 2. In one embodiment, the secondmolecular sieve has a framework type of at least one of FAU, *BEA, MFI,MTW, and any combination thereof.

Suitable medium pore molecular sieves having a Constraint Index of 2-12(as defined in U.S. Pat. No. 4,016,218), include ZSM-5, ZSM-11, ZSM-12,ZSM-22, ZSM-23, ZSM-35, and ZSM-48. ZSM-5 is described in detail in U.S.Pat. No. 3,702,886 and Re. 29,948. ZSM-11 is described in detail in U.S.Pat. No. 3,709,979. ZSM-12 is described in U.S. Pat. No. 3,832,449.ZSM-22 is described in U.S. Pat. No. 4,556,477. ZSM-23 is described inU.S. Pat. No. 4,076,842. ZSM-35 is described in U.S. Pat. No. 4,016,245.ZSM-48 is more particularly described in U.S. Pat. No. 4,234,231. Theentire contents of all the above patent specifications are incorporatedherein by reference.

Suitable large pore molecular sieves include zeolite beta, zeolite Y,Ultrastable Y (USY), Dealuminized Y (Deal Y), mordenite, ZSM-3, ZSM-4,ZSM-18, and ZSM-20. Zeolite ZSM-14 is described in U.S. Pat. No.3,923,636. Zeolite ZSM-20 is described in U.S. Pat. No. 3,972,983.Zeolite beta is described in U.S. Pat. No. 3,308,069, and Re. No.28,341. Low sodium Ultrastable Y molecular sieve (USY) is described inU.S. Pat. Nos. 3,293,192 and 3,449,070. Dealuminized Y zeolite (Deal Y)may be prepared by the method found in U.S. Pat. No. 3,442,795. ZeoliteUHP-Y is described in U.S. Pat. No. 4,401,556. Rare earth exchanged Y(REY) is described in U.S. Pat. No. 3,524,820. Mordenite is a naturallyoccurring material but is also available in synthetic forms, such asTEA-mordenite (i.e., synthetic mordenite prepared from a reactionmixture comprising a tetraethylammonium directing agent). TEA-mordeniteis disclosed in U.S. Pat. Nos. 3,766,093 and 3,894,104. The entirecontents of all the above patent specifications are incorporated hereinby reference.

The Constraint Index is a convenient measure of the extent to which analuminosilicate or molecular sieve provides controlled access tomolecules of varying sizes to its internal structure. For example,aluminosilicates which provide a highly restricted access to and egressfrom its internal structure have a high value for the constraint index,and aluminosilicates of this kind usually have pores of small size, e.g.less than 5 Angstroms. On the other hand, aluminosilicates which providerelatively free access to the internal aluminosilicate structure have alow value for the constraint index, and usually pores of large size. Themethod by which Constraint Index may be determined is described fully inU.S. Pat. No. 4,016,218, which is incorporated herein by reference.

In some embodiments, the catalyst composition further comprises at least5 wt % of a second molecular sieve having a *BEA framework type based onthe total weight of the catalyst composition.

The stability of the catalyst(s) used in the present process may beincreased by steaming. U.S. Pat. Nos. 4,663,492; 4,594,146; 4,522,929;and 4,429,176, describe conditions for the steam stabilization ofzeolite catalysts which may be utilized to steam-stabilize the catalyst.Reference is made to these patents for a detailed description of thesteam stabilization technique for use with the present catalysts. Thesteam stabilization conditions typically include contacting the catalystwith, e.g., 5-100% steam at a temperature of at least about 300° C.(e.g., 300°-650° C.) for at least one hour (e.g., 1-200 hours) at apressure of 101-2,500 kPa-a. In a more particular embodiment, thecatalyst may be made to undergo steaming with 75-100% steam at 315°-500°C. and atmospheric pressure for 2-25 hours. The steaming of the catalystmay take place under conditions sufficient to initially increase theAlpha Value of the catalyst, the significance of which is discussedbelow, and produce a steamed catalyst having an enhanced Alpha Value. Ifdesired, steaming may be continued to subsequently reduce the AlphaValue from the higher Alpha Value to an Alpha Value which issubstantially the same as the Alpha Value of the unsteamed catalyst.

The alpha value test is a measure of the cracking activity of a catalystand is described in U.S. Pat. No. 3,354,078 and in the Journal ofCatalysis, Vol. 4, p. 527 (1965); Vol. 6, p. 278 (1966); and Vol. 61, p.395 (1980), each incorporated herein by reference as to thatdescription. The experimental conditions of the test used herein includea constant temperature of 538° C. and a variable flow rate as describedin detail in the Journal of Catalysis, Vol. 61, p. 395.

In some aspects of this disclosure, the binder comprises at least onecompound of Group 1 to Group 17 element, preferably the binder comprisestitanium compound, alumina compound, silicon compound, or any mixturethereof, more preferably the binder is selected from a group consistingof titanium oxide, titanium hydroxide, titanium sulfate, titaniumphosphate, aluminum oxide, aluminum hydroxide, aluminum sulfate,aluminum phosphate, silica, silicates, aluminosilicates,titanosilicates, titanoaluminosilicates, aluminophosphates,metallophosphates, metalloaluminophosphates, silicoaluminophosphates,and any combination thereof. Preferably, the catalyst composition has atleast 1 wt % of the binder based on the total weight of the catalystcomposition.

In yet other embodiments, this disclosure relates to a process forpreparing the catalyst composition of this disclosure, the processcomprises (a) providing the crystalline MCM-22 family molecular sieveand the binder to form a mixture; and (b) forming the mixture into thecatalyst composition. The crystals prepared by the instant invention canbe shaped into a wide variety of particle sizes. Generally, theparticles can be in the form of a powder, a granule, or a moldedproduct, such as an extrudate. In cases where the catalyst is molded,such as by extrusion, the crystals can be extruded before drying orpartially dried and then extruded. In a preferred embodiment, theforming step comprises extruding. In another preferred embodiment, thecatalyst composition has a shape of quadrulobe. In one embodiment, thecatalyst composition has at least 65 wt % of the crystalline MCM-49based on the total weight of the catalyst composition.

In some embodiments, the catalyst composition may further comprise amaterial resistant to the temperatures and other conditions employed inorganic conversion processes. Such materials include clays, silicaand/or metal oxides such as alumina. The latter may be either naturallyoccurring or in the form of gelatinous precipitates or gels includingmixtures of silica and metal oxides. These materials may be incorporatedinto naturally occurring clays, e.g., bentonite and kaolin, to improvethe crush strength of the catalyst under commercial operatingconditions. The materials, i.e. clays, oxides, etc., function as bindersfor the catalyst. It is desirable to provide a catalyst having goodcrush strength because in commercial use it is desirable to prevent thecatalyst from breaking down into powder-like materials.

Naturally occurring clays which can be composited with the crystallinemolecular sieve include the montmorillonite and kaolin family, whichfamilies include the subbentonites, and the kaolins commonly known asDixie, McNamee, Georgia and Florida clays or others in which the mainmineral constituent is halloysite, kaolinite, dictite, narcite, oranauxite. Such clays can be used in the raw state as originally mined orinitially subjected to calcination, acid treatment or chemicalmodification. Binders useful for compositing with the present crystalalso include inorganic oxides, notably alumina.

In addition to the foregoing materials, the crystalline molecular sievecan be composited with a porous matrix material such as silica-alumina,silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia,silica-titania as well as ternary compositions such assilica-alumina-thoria, silica-alumina-zirconia silica-alumina-magnesiaand silica-magnesia-zirconia.

The relative proportions of finely divided crystalline molecular sieveand inorganic oxide matrix vary widely, with the crystal content rangingfrom about 1 to about 99 percent by weight and more usually,particularly when the composite is prepared in the form of beads, in therange of about 20 to about 80 wt % of the composite.

A summary of the molecular sieves and/or zeolites, in terms ofproduction, modification and characterization of molecular sieves, isdescribed in the book “Molecular Sieves—Principles of Synthesis andIdentification”; (R. Szostak, Blackie Academic & Professional, London,1998, Second Edition). In addition to molecular sieves, amorphousmaterials, chiefly silica, aluminum silicate and aluminum oxide, havebeen used as adsorbents and catalyst supports. A number of long-knownforming techniques, like spray drying, prilling, pelletizing andextrusion, have been and are being used to produce macrostructures inthe form of, for example, spherical particles, extrudates, pellets andTablets of both micropores and other types of porous materials for usein catalysis, adsorption and ion exchange. A summary of these techniquesis described in “Catalyst Manufacture,” A. B. Stiles and T. A. Koch,Marcel Dekker, New York, 1995.

Alkylation Reactions

In another embodiment, this disclosure discloses a process foralkylating an aromatic hydrocarbon with an alkylating agent to producean alkylated aromatic product, the process comprises contacting thearomatic hydrocarbon and the alkylating agent with the catalystcomposition under alkylation conditions effective to alkylate thearomatic hydrocarbon with the alkylating agent to form an effluentcomprising the alkylated aromatic product. In some preferredembodiments, the aromatic hydrocarbon comprises benzene, the alkylatingagent comprises ethylene, and the alkylated aromatic product comprisesethylbenzene. In other preferred embodiments, the aromatic hydrocarboncomprises benzene, the alkylating agent comprises propylene, and thealkylated aromatic product comprises cumene.

The crystalline MCM-22 family molecular sieve(s) of this disclosure arealso useful catalyst for transalkylations, such as, for example,polyalkylbenzene transalkylations.

Substituted aromatic compounds which may be used for the inventionshould possess at least one hydrogen atom directly bonded to thearomatic nucleus. The aromatic rings may be substituted with one or morealkyl, aryl, alkaryl, alkoxy, aryloxy, cycloalkyl, halide, and/or othergroups which do not interfere with the alkylation reaction.

Suitable aromatic compounds that may be used for this invention includebenzene, naphthalene, anthracene, naphthacene, perylene, coronene, andphenanthrene, with benzene being preferred.

Suitable alkyl substituted aromatic compounds that may be used for thisinvention include toluene, xylene, isopropylbenzene, normalpropylbenzene, alpha-methylnaphthalene, ethylbenzene, mesitylene,durene, cymenes, butylbenzene, pseudocumene, o-diethylbenzene,m-diethylbenzene, p-diethylbenzene, isoamylbenzene, isohexylbenzene,pentaethylbenzene, pentamethylbenzene; 1,2,3,4-tetraethylbenzene;1,2,3,5-tetramethylbenzene; 1,2,4-triethylbenzene;1,2,3-trimethylbenzene, m-butyltoluene; p-butyltoluene;3,5-diethyltoluene; o-ethyltoluene; p-ethyltoluene; m-propyltoluene;4-ethyl-m-xylene; dimethylnaphthalenes; ethylnaphthalene;2,3-dimethylanthracene; 9-ethylanthracene; 2-methylanthracene;o-methylanthracene; 9,10-dimethylphenanthrene; and3-methyl-phenanthrene. Higher molecular weight alkylaromatichydrocarbons may also be used as starting materials and include aromatichydrocarbons such as are produced by the alkylation of aromatichydrocarbons with olefin oligomers. Such products are frequentlyreferred to in the art as alkylate and include hexylbenzene,nonylbenzene, dodecylbenzene, pentadecylbenzene, hexyltoluene,nonyltoluene, dodecyltoluene, pentadecytoluene, etc. Very often alkylateis obtained as a high boiling fraction in which the alkyl group attachedto the aromatic nucleus varies in size from about C₆ to about C₁₂.

Reformate streams that may contain substantial quantities of benzene,toluene and/or xylene may be particularly suitable feed for the processof this invention. Although the process is particularly directed to theproduction of ethylbenzene from polymer grade and dilute ethylene, it isequally applicable to the production of other C₇-C₂₀ alkylaromaticcompounds, such as cumene, as well as C₆+ alkylaromatics, such as C₈-C₁₆linear and near linear alkylbenzenes.

Suitable alkylating agent(s) that may be used in this disclosurecomprise alkene compound(s), alcohol compound(s), and/oralkylbenzene(s), and mixtures thereof. Other suitable alkylating agentsthat may be useful in the process of this disclosure generally includeany aliphatic or aromatic organic compound having one or more availablealkylating aliphatic groups capable of reaction with the alkylatablearomatic compound. Examples of suitable alkylating agents are C₂-C₁₆olefins such as C₂-C₅ olefins, viz., ethylene, propylene, the butenes,and the pentenes; C₁-C₁₂ alkanols (inclusive of monoalcohols,dialcohols, trialcohols, etc.), preferably C₁-C₅ alkanols, such asmethanol, ethanol, the propanols, the butanols, and the pentanols;C₂-C₂₀ ethers, e.g., C₂-C₅ ethers including dimethylether anddiethylether; aldehydes such as formaldehyde, acetaldehyde,propionaldehyde, butyraldehyde, and n-valeraldehyde; and alkyl halidessuch as methyl chloride, ethyl chloride, the propyl chlorides, the butylchlorides, and the pentyl chlorides, polyalkylated aromatic compound(s),e.g., bi-alkylated benzenes (e.g., bi-ethylbenzene(s) orbi-isopropylbenzenes) and tri-alkylated benzene(s) (e.g.,tri-ethylbenzenes or tri-isopropylbenzenes), and so forth. Thus thealkylating agent may preferably be selected from the group consisting ofC₂-C₅ olefins, C₁-C₅ alkanols, bi-ethylbenzene(s),bi-isopropylbenzene(s), tri-ethylbenzene(s) and/ortri-isopropylbenzene(s). The alkylating agent includes a concentratedalkene feedstock (e.g., polymer grade olefins) and a dilute alkenefeedstock (e.g., catalytic cracking off-gas).

Suitable alkyl substituted aromatic compounds which may be prepared fromthe alkylation process of the present invention include toluene, xylene,isopropylbenzene (cumene), normal propylbenzene,alpha-methylnaphthalene, ethylbenzene, mesitylene, durene, cymenes,butylbenzene, pseudocumene, o-diethylbenzene, m-diethylbenzene,p-diethylbenzene, isoamylbenzene, isohexylbenzene, pentaethylbenzene,pentamethylbenzene; 1,2,3,4-tetraethylbenzene;1,2,3,5-tetramethylbenzene; 1,2,4-triethylbenzene;1,2,3-trimethylbenzene, m-butyltoluene; p-butyltoluene;3,5-diethyltoluene; o-ethyltoluene; p-ethyltoluene; m-propyltoluene;4-ethyl-m-xylene; dimethylnaphthalenes; ethylnaphthalene;2,3-dimethyl,anthracene; 9-ethylanthracene; 2-methylanthracene;o-methylanthracene; 9,10-dimethylphenanthrene; and3-methyl-phenanthrene. Preferably, the alkylated aromatic productcomprises monoalkylbenzene. Higher molecular weight alkylaromatichydrocarbons may also be used as starting materials and include aromatichydrocarbons such as are produced by the alkylation of aromatichydrocarbons with olefin oligomers. Such products are frequentlyreferred to in the art as alkylate and include hexylbenzene,nonylbenzene, dodecylbenzene, pentadecylbenzene, hexyltoluene,nonyltoluene, dodecyltoluene, pentadecyltoluene, etc. Very oftenalkylate is obtained as a high boiling fraction in which the alkyl groupattached to the aromatic nucleus varies in size from about C₆ to aboutC₁₆.

The alkylation reaction is carried out with the alkylatable aromaticcompound and the alkylating agent in the reaction zone under alkylationor transalkylation conditions. The alkylation or transalkylationconditions include a temperature of 100 to 285° C. and a pressure of 689to 4601 kPa-a, preferably, a pressure of 1500 to 3000 kPa-a, a WHSVbased on alkylating agent (e.g., alkene) for overall reactor of 0.1 to10 hr⁻¹, preferably, 0.2 to 2 hr⁻¹, more preferably, 0.5 to 1 hr⁻¹, or aWHSV based on both alkylating agent and alkylatable aromatics foroverall reactor of 10 to 100 hr⁻¹, preferably, 20 to 50 hr⁻¹. Thealkylatable aromatic compound is alkylated with the alkylating agent(e.g., alkene) in the presence of an alkylation or transalkylationcatalyst in a reaction zone or a plurality of reaction zones. Thereaction zone(s) are preferably located in a single reactor vessel, butmay include another reaction zone having an alkylation ortransalkylation catalyst bed, located in separate vessel which may be aby-passable and which may operate as a reactive guard bed. The catalystcomposition used in the reactive guard bed may be different from thecatalyst composition used in the reaction zone. The catalyst compositionused in the reactive guard bed may have multiple catalyst compositions.At least one reaction zone, and normally each reaction zone, ismaintained under conditions effective to cause alkylation of thealkylatable aromatic compound with the alkylating agent in the presenceof an alkylation or transalkylation catalyst.

The effluent from the reaction zone comprises the desired alkylatedaromatic product, unreacted alkylatable aromatic compound, any unreactedalkylating agent (e.g., alkene, alkene conversion is expected to be atleast 90 mol. %, preferably, about 98-99.9999 mol. %) and the alkanecomponent and the other impurities. In one embodiment, at least aportion of the effluent is fed to another reaction zone where analkylating agent is added for reaction with the unreacted alkylatablearomatic compound with an alkylation or transalkylation catalyst.Furthermore, at least a portion the effluent from any of the reactionzone(s) may be fed directly or indirectly to a transalkylation unit.

In addition to, and upstream of, the reaction zones, a by-passablereactive or unreactive guard bed may normally be located in a reactorseparate from the alkylation reactor. Such guard bed may also be loadedwith an alkylation or transalkylation catalyst, which may be the same ordifferent from the catalyst used in the reaction zone(s). Such guard bedis maintained from under ambient conditions, or at suitable alkylationor transalkylation conditions. At least a portion of alkylatablearomatic compound, and optionally at least a portion of the alkylatingagent, are passed through the unreactive or reactive guard bed prior toentry into the reaction zone. These guard beds not only serve to affectthe desired alkylation reaction, but is also used to remove any reactiveimpurities in the feeds, such as nitrogen compounds, which couldotherwise poison the remainder of the alkylation or transalkylationcatalyst. The catalyst in the reactive or unreactive guard bed istherefore subject to more frequent regeneration and/or replacement thanthe remainder of the alkylation or transalkylation catalyst, and hencethe guard bed is typically provided with a by-pass circuit so that thealkylation feed(s) may be fed directly to the series connected reactionzones in the reactor while the guard bed is out of service. The reactiveor unreactive guard bed may be operated in co-current upflow or downflowoperation.

The reaction zone(s) used in the process of the present invention istypically operated so as to achieve essentially complete conversion ofthe alkene. However, for some applications, it may be desirable tooperate at below 100% alkene conversion. The employment of a separatefinishing reactor downstream of the reaction zone(s) may be desirableunder certain conditions. The finishing reactor would also containalkylation or transalkylation catalyst, which could be the same ordifferent from the catalyst used in other reaction zones in thealkylation or transalkylation reactor(s) and may be maintained under atleast partially liquid phase or alternately vapor phase alkylation ortransalkylation conditions. The polyalkylated aromatic compounds in theeffluents may be separated for transalkylation with alkylatable aromaticcompound(s). The alkylated aromatic compound is made by transalkylationbetween polyalkylated aromatic compounds and the alkylatable aromaticcompound.

The alkylation or transalkylation reactor(s) used in the process of thepresent invention may be highly selective to the desired monoalkylatedproduct, such as ethylbenzene, but typically produces at least somepolyalkylated species. In one embodiment, the effluent from the finalalkylation reaction zone is subjected to a separation step to recoverpolyalkylated aromatic compound(s). In another embodiment, at least aportion of the polyalkylated aromatic compound is supplied to atransalkylation reactor which may be separate from the alkylationreactor. The transalkylation reactor produces an effluent which containsadditional monoalkylated product by reacting the polyalkylated specieswith an alkylatable aromatic compound. At least a portion of theseeffluents may be separated to recover the alkylated aromatic compound(monoalkylated aromatic compound and/or polyalkylated aromaticcompound).

Particular conditions for carrying out the alkylation of benzene withethylene at least partially in liquid phase may have a temperature offrom about 120 to 285° C., preferably, a temperature of from about 150to 260° C., a pressure of 689 to 4601 kPa-a, preferably, a pressure of1500 to 4137 kPa-a, a WHSV based on total ethylene and total catalystfor overall reactor of 0.1 to 10 hr⁻¹, preferably, 0.2 to 2 hr⁻¹, morepreferably, 0.5 to 1 hr⁻¹, or a WHSV based on both total ethylene andbenzene, and total catalyst for overall reactor of 10 to 100 hr⁻¹,preferably, 20 to 50 hr⁻¹, and a molar ratio of benzene to ethylene fromabout 1 to about 10.

Particular conditions for carrying out the at least partially in liquidphase alkylation of benzene with propylene may include a temperature offrom about 80 to 160° C., a pressure of about 680 to about 4800 kPa-a;preferably from about 100 to 140° C. and pressure of about 2000 to 3000kPa-a, a WHSV based on propylene of from about 0.1 about 10 hr⁻¹, and amolar ratio of benzene to ethylene from about 1 to about 10.

Where the alkylation system includes a reactive guard bed, it ismaintained under at least partial in liquid phase conditions. The guardbed will preferably operate at a temperature of from about 120 to 285°C., preferably, a temperature of from about 150 to 260° C., a pressureof 689 to 4601 kPa-a, preferably, a pressure of 1500 to 4137 kPa-a, aWHSV based on total ethylene and the total amount of catalyst for theoverall reactor of 0.1 to 10 hr⁻¹, preferably, 0.2 to 2 hr⁻¹, morepreferably, 0.5 to 1 hr⁻¹, or a WHSV based on both total ethylene andtotal benzene, and the total amount of catalyst for the overall reactorof 10 to 100 hr⁻¹, preferably, 20 to 50 hr⁻¹, and a molar ratio ofbenzene to ethylene from about 1 to about 10.

The transalkylation reaction may take place under at least partially inliquid phase conditions. Particular conditions for carrying out the atleast partially in liquid phase transalkylation of polyalkylatedaromatic compound(s), e.g., polyethylbenzene(s) orpolyisopropylbenzene(s), with benzene may include a temperature of fromabout 100° to about 300° C., a pressure of 696 to 4137 kPa-a, a WHSVbased on the weight of the polyalkylated aromatic compound(s) feed tothe alkylation reaction zone of from about 0.5 to about 100 hr⁻¹ and amolar ratio of benzene to polyalkylated aromatic compound(s) of from 1:1to 30:1, preferably, 1:1 to 10:1, more preferably, 1:1 to 5:1.

In another embodiment, the transalkylation reaction may take place undervapor phase conditions. Particular conditions for carrying out the vaporphase transalkylation of polyalkylated aromatic compound(s), e.g.,polyethylbenzene(s) or polyisopropylbenzene(s), with benzene may includea temperature of from about 350 to about 450° C., a pressure of 696 to1601 kPa-a, a WHSV based on the weight of the polyalkylated aromaticcompound(s) feed to the reaction zone of from about 0.5 to about 20hr⁻¹, preferably, from about 1 to about 10 hr⁻¹, and a molar ratio ofbenzene to polyalkylated aromatic compound(s) of from 1:1 to 5:1,preferably, 2:1 to 3:1.

In some embodiments, this disclosure relates to:

-   Paragraph 1. A catalyst composition comprising:    -   (a) a crystalline MCM-22 family molecular sieve; and    -   (b) a binder,    -   wherein the catalyst composition is characterized by a        cumulative extra-molecular sieve pore volume greater than or        equal to 0.122 ml/g for pores having a pore diameter ranging        from about 2 nm to about 8 nm, wherein the pore volume is        measured by N₂ porosimetry.-   Paragraph 2. The catalyst composition of paragraph 1, wherein the    extra-molecular sieve porosity greater than or equal to 0.125 ml/g.-   Paragraph 3. The catalyst composition of paragraph 1, wherein the    extra-molecular sieve porosity greater than or equal to 0.13 ml/g.-   Paragraph 4. The catalyst composition of any preceding paragraph,    wherein the extra-molecular sieve porosity less than or equal to 5    ml/g.-   Paragraph 5. The catalyst composition of any preceding paragraph,    further comprising a second molecular sieve having a Constraint    Index of less than 12.-   Paragraph 6. The catalyst composition of any preceding paragraph,    further comprising a second molecular sieve having a Constraint    Index of less than 2.-   Paragraph 7. The catalyst composition of paragraph 5 or 6, wherein    the second molecular sieve has a framework type of at least one of    FAU, *BEA, MFI, MTW, and any combination thereof.-   Paragraph 8. The catalyst composition of any preceding paragraph    wherein the crystalline MCM-22 family molecular sieve comprises at    least one of ERB-1, ITQ-2, PSH-3, SSZ-25, MCM-22, MCM-36, MCM-49,    MCM-56, ITQ-1, ITQ-30, and any combination thereof.-   Paragraph 9. The catalyst composition of any preceding paragraph,    wherein the binder comprises at least one compound of Group 1 to    Group 17 element.-   Paragraph 10. The catalyst composition of any preceding paragraph,    wherein the binder comprises titanium compound, alumina compound,    silicon compound, or any mixture thereof.-   Paragraph 11. The catalyst composition of any preceding paragraph,    wherein the binder is selected from a group consisting of titanium    oxide, titanium hydroxide, titanium sulfate, titanium phosphate,    aluminum oxide, aluminum hydroxide, aluminum sulfate, aluminum    phosphate, silica, silicates, aluminosilicates, titanosilicates,    titanoaluminosilicates, aluminophosphates, metallophosphates,    metalloaluminophosphates, silicoaluminophosphates, and any    combination thereof.-   Paragraph 12. The catalyst composition of any preceding paragraph    having at least 50 wt % of the crystalline MCM-22 family molecular    sieve based on the total weight of the catalyst composition.-   Paragraph 13. A process for alkylation or transalkylation of an    alkylatable aromatic compound with an alkylating agent to produce a    monoalkylated aromatic compound, comprising the steps of:    -   (a) contacting at least one the alkylatable aromatic compound        and at least one the alkylating agent with a catalyst        composition under suitable alkylation or transalkylation        conditions in at least one reaction zone, to produce at least        one effluent which comprises the monoalkylated aromatic compound        and a monoalkylated aromatic compound selectivity; the catalyst        composition comprising:        -   (i) a crystalline MCM-22 family molecular sieve; and        -   (ii) a binder,        -   wherein the catalyst composition is characterized by an            extra-molecular sieve porosity greater than or equal to            0.122 ml/g for pores having a pore diameter ranging from            about 2 nm to about 8 nm, wherein the porosity is measured            by N₂ porosimetry.    -   wherein the monoalkylated aromatic compound selectivity of the        catalyst composition is greater than the monoalkylated aromatic        compound selectivity of a catalyst composition having an        extra-molecular sieve porosity outside the range of the catalyst        composition the for pores having a pore diameter ranging from        about 2 nm to about 8 nm, when the reaction zone is operated        under equivalent alkylation or transalkylation conditions.-   Paragraph 14. The process of paragraph 13, wherein the    extra-molecular sieve porosity greater than or equal to 0.125 ml/g.-   Paragraph 15. The process of paragraph 13 or 14, wherein the    extra-molecular sieve porosity greater than or equal to 0.13 ml/g.-   Paragraph 16. The process of any one of paragraphs 13-15, further    comprising a second molecular sieve catalyst having a Constraint    Index of less than 12.-   Paragraph 17. The process of any one of paragraphs 13-16, further    comprising a second molecular sieve catalyst having a Constraint    Index of less than 2.-   Paragraph 18. The process of any one of paragraphs 13-17, wherein    the catalyst composition consists essentially of a MCM-22 family    molecular sieve.-   Paragraph 19. The process of paragraph 18, wherein the MCM-22 family    molecular sieve is ERB-1, ITQ-1, ITQ-2, ITQ-30, PSH-3, SSZ-25,    MCM-22, MCM-36, MCM-49, MCM-56, or any combination thereof.-   Paragraph 20. The process of paragraph 16, wherein the second    molecular sieve comprises a molecular sieve selected from a group    consisting of zeolite beta, zeolite Y, Ultrastable Y, Dealuminized    Y, rare earth exchanged Y, mordenite, TEA-mordenite, silicalite,    ZSM-3, ZSM-4, ZSM-5, ZSM-11, ZSM-12, ZSM-14, ZSM-18, ZSM-20, ZSM-22,    ZSM-23, ZSM-35, and ZSM-48.-   Paragraph 21. The process of any one of paragraphs 13-20, further    comprising a finishing reactor downstream of the reaction zone.-   Paragraph 22. The process of any one of paragraphs 13-21, wherein    the suitable alkylation or transalkylation conditions include a    temperature from about 100° C. to about 400° C., a pressure from    about 20.3 to 4500 kPa-a, a WHSV from about 0.1 to about 10 hr⁻¹,    and a molar ratio of the alkylatable compound over the alkylating    agent from about 0.1:1 to 50:1.-   Paragraph 23. The process of any one of paragraphs 13-22, wherein    the monoalkylated aromatic compound comprises ethylbenzene, the    alkylatable aromatic compound comprises benzene, and the alkylating    agent comprises ethylene.-   Paragraph 24. The process of any one of paragraphs 13-23, wherein    the monoalkylated aromatic compound comprises cumene, the    alkylatable aromatic compound comprises benzene, and the alkylating    agent comprises propylene.-   Paragraph 25. A process for preparing the catalyst composition of    any one of paragraphs 1-12 comprising:    -   (a) providing the crystalline MCM-22 family molecular sieve and        the binder to form a mixture; and    -   (b) forming the mixture into the catalyst composition.-   Paragraph 26. The process of paragraph 25, wherein the forming step    comprises extruding.-   Paragraph 27. The process of any one paragraphs 25-26, wherein the    catalyst composition has a shape of quadrulobe.-   Paragraph 28. The process of any one paragraphs 25-27, wherein the    catalyst composition has at least 65 wt % of crystalline MCM-22    family molecular sieve based on the total weight of the catalyst    composition.-   Paragraph 29. The process of any one paragraphs 25-28, wherein the    catalyst composition further comprises at least 5 wt % of a    molecular sieve having a *BEA framework type based on the total    weight of the catalyst composition.

These and other facets of the present invention are exemplified by thefollowing Examples.

Testing Procedures

Feed Pretreatment

Benzene (99.96 wt %) was obtained from the ExxonMobil Baytown Chemicalplant. The benzene was passed through a pretreatment vessel (2 L Hokevessel) containing absorbent materials from inlet to outlet. Allabsorbent feed pretreatment materials were dried in a 260° C. oven for12 hours before using.

Polymer grade propylene was obtained from Scott Specialty Gases(Pasadena, Tex., USA). Propylene was passed through a 300 ml vesselcontaining absorbents which were dried in a 260° C. oven for 12 hoursbefore using.

Ultra high purity grade Nitrogen was obtained from Scott SpecialtyGases. Nitrogen was passed through a 300 ml vessel containing absorbentswhich were dried at 260° C. for 12 hours before using.

Catalyst Preparation and Loading

MCM-22 catalyst was prepared according to U.S. Pat. No. 4,954,325, thewhole content of which is incorporated herein as reference. MCM-49catalyst was prepared according to U.S. Pat. No. 5,236,575, the wholecontent of which is incorporated herein as reference.

Titania was obtained from Degussa Corporation (Degussa AG, PO Box 30 2043, 40402 Dusseldorf, Germany) as AEROXIDE® TiO₂ P25 (hereinafter “P25titania”). Alumina was obtained from UOP LLC (UOP LLC, 25 East AlgonquinRoad, Des Plaines, Ill. 60017-5017, U.S.A.) as Versal-300 alumina.

Extrusion was performed on Bonnot single screw extruder (The BonnotCompany, 1520 Corporate Woods Parkway, Uniontown, Ohio 44685, U.S.A.).Organic extrusion aid, poly vinyl alcohol (hereinafter “PVA”) wasobtained from Celanese as Celvol 603. Scanning Electron Microscope (SEM)images were obtained on a HITACHI 54800 Field Emission Scanning ElectronMicroscope (SEM).

0.5 grams of catalyst was dried in air at 260° C. for 2 hours. Thecatalyst was removed immediately after drying. The bottom of a catalystbasket was packed with quartz chips followed by loading of one gram ofcatalyst into basket on top of the quartz chips. The catalyst was thencovered by additional quartz chips. The catalyst basket containing thecatalyst and quartz chips was dried at 260° C. in air for about 16hours.

Before each experiment the reactor and all lines were cleaned with asuitable solvent (such as toluene) followed by flowing of air aftercleaning to remove all cleaning solvent. The catalyst basket containingthe catalyst and quartz chips was placed in reactor immediately afterdrying.

A 300 ml Parr® batch reaction vessel (Series 4563 mini Bench top reactorwith a static catalyst basket, Parr Instrument Company, Moline, Ill.USA) equipped with a stir rod and static catalyst basket was used forthe activity and selectivity measurements. The reaction vessel wasfitted with two removable vessels for the introduction of benzene andpropylene respectively.

Catalyst Activity and Selectivity

The activity and selectivity of a catalyst were measured based onbenzene alkylation with propylene. Catalyst activity was calculatedusing the second order rate constant for the formation of cumene underthe reaction conditions (temperature 130° C. and pressure 2170 kPa-a).Reaction rate-constants were calculated using methods known to thoseskilled in the art. See “Principles and Practice of HeterogeneousCatalyst”, J. M. Thomas, W. J. Thomas, VCH, 1st Edition, 1997, thedisclosure of which is incorporated herein by reference. Catalystselectivity was calculated using the weight ratio of cumene producedover di-isopropyl benzenes produced under the reaction conditions(temperature 130° C. and pressure 2170 kPa-a).

The reactor was purged with 100 ml/min of the treated ultra high puritynitrogen, N₂, for 2 hours at 170° C. Then, the reactor temperature wasreduced to 130° C. under nitrogen flow. All inlets and outlets of thereactor were closed off afterward. Pretreated benzene (156.1 gram) wastransferred into the reactor under 791 kPa-a ultra high purity nitrogenblanket. The reactor was stirred at 500 rpm for 1 hour. Pretreatedliquid propylene (28.1 gram) under 2170 kPa-a ultra high purity nitrogenis then transferred to the reactor. The reactor was maintained at 2170kPa-a by the 2170 kPa-a ultra high purity nitrogen. Liquid samples weretaken at 30, 60, 120, 150, 180 and 240 min after addition of thepropylene.

Jet milling was performed on a Micron Master Jet Mill (Jet Pulverizer,in Moorestown, N.J., USA).

The N₂ pore size distribution was obtained on a Tristar 3000 GasAdsorption Analyzer unit (Micromeritics®, Norcross, Ga., USA) from thedesorption leg of the N₂ isotherm. The pore volumes for pore sizes inthe 2-8 nm range were summed up to obtain cumulative pore volume.

Example 1

MCM-49 was extruded in a 5.08 cm (2″) extruder according to thefollowing formulation: mixture of MCM-49 crystal and Versal-300 alumina(weight ratio 80:20) extruded with 0.05 wt % PVA (based on the combinedweight of MCM-49 crystal, Versal-300 alumina, and PVA) to 0.127 cm (1/20″) extrudate. This extrudate was then pre-calcined in nitrogen at510° C., ammonium exchanged with ammonium nitrate, and calcined in anair/N₂ mixture at 538° C. The catalyst from Example 1 was tested in thebatch autoclave liquid phase benzene alkylation test and results arelisted in Table 1.

Example 2

MCM-49 was extruded in a 5.08 cm (2″) extruder according to thefollowing formulation: mixture of MCM-49 crystal and Condea alumina(weight ratio 80:20) extruded with 0.05 wt % PVA (based on the combinedweight of MCM-49 crystal, Versal-300 alumina, and PVA) to 0.127 cm (1/20″) extrudate. This extrudate was then pre-calcined in nitrogen at510° C., ammonium exchanged with ammonium nitrate, and calcined in anair/N₂ mixture at 538° C. The catalyst from Example 2 was tested in thebatch autoclave liquid phase benzene alkylation test and results arelisted in Table 1.

Example 3

MCM-49 was jet pulverized (also called Jet milling) to reduce theaverage crystal aggregate size of the MCM-49 material from about 16micron to about than 1.2 micron at high velocity mixing and extruded ina 5.08 cm (2″) extruder according to the following formulation: mixtureof MCM-49 crystal and Versal-300 alumina (weight ratio 80:20) extrudedwith 0.05 wt % PVA (based on the combined weight of MCM-49 crystal,Versal-300 alumina, and PVA) to 0.127 cm ( 1/20″) extrudate. Thisextrudate was then pre-calcined in nitrogen at 510° C., ammoniumexchanged with ammonium nitrate, and calcined in an air/N₂ mixture at538° C. The catalyst from Example 3 was tested in the batch autoclaveliquid phase benzene alkylation test and results are listed in Table 1.

Example 4

MCM-49 was extruded in a 5.08 cm (2″) extruder according to thefollowing formulation: mixture of MCM-49 crystal and Ultrasil silica(weight ratio 80:20) extruded with 2 wt % PVA (based on the combinedweight of MCM-49 crystal, silica, and PVA) to 0.127 cm ( 1/20″)extrudate. This extrudate was then pre-calcined in nitrogen at 510° C.,ammonium exchanged with ammonium nitrate, and calcined in an air/N₂mixture at 538° C. The catalyst from Example 4 was tested in the batchautoclave liquid phase benzene alkylation test and results are listed inTable 1.

Table 1 lists the activity and selectivity of catalysts from examples 2,3, 4 normalized to the base case in example 1 as well as the cumulativepore volume in the 2-8 nm range obtained from N₂ porosimetry.

Activity Selectivity to cumene Cumulative Normalized normalized toexample pore volume in Example to example 1 1 (cumene/DiPB) 2-8 nmrange, ml/g Example 1 100 100 0.121 Example 2 104 157 0.153 Example 3117 150 0.132 Example 4 99 65 0.031

As shown in the Table 1, all catalysts had similar activity, samezeolite content but had widely varying selectivities as measured by theweight ratio of cumene over Di-isopropyl benzene make. Poorermono-alkylated aromatics selectivity (examples 1 and 4) is correlatedwith the low pore volume in the 2-8 nm range whereas improvedselectivity (examples 2, 3) are correlated with increased pore volume inthe 2-8 nm range.

1. A process for alkylation or transalkylation of an alkylatablearomatic compound with an alkylating agent to produce a monoalkylatedaromatic compound, comprising the steps of: (a) contacting at least onesaid alkylatable aromatic compound and at least one said alkylatingagent with a catalyst composition under suitable alkylation ortransalkylation conditions in at least one reaction zone, to produce atleast one effluent which comprises said monoalkylated aromatic compoundand a monoalkylated aromatic compound selectivity; said catalystcomposition comprising: (i) a crystalline MCM-22 family molecular sieve;and (ii) a binder, said binder comprising a condea alumina wherein saidcatalyst composition is characterized by a cumulative pore volume ofgreater than or equal to 0.153 ml/g for pores having a pore diameterranging from about 2 nm to about 8 nm, wherein said porosity is measuredby N₂ porosimetry, wherein the monoalkylated aromatic compoundselectivity of said catalyst composition is greater than themonoalkylated aromatic compound selectivity of a catalyst compositionhaving an extra-molecular sieve porosity outside the range of saidcatalyst composition the for pores having a pore diameter ranging fromabout 2 nm to about 8 nm, when said reaction zone is operated underequivalent alkylation or transalkylation conditions.
 2. The process ofclaim 1, further comprising a second molecular sieve catalyst having aConstraint Index of less than
 12. 3. The process of claim 1, furthercomprising a second molecular sieve catalyst having a Constraint Indexof less than
 2. 4. The process of claim 1, wherein said catalystcomposition consists essentially of a MCM-22 family molecular sieve. 5.The process of claim 4, wherein said crystalline MCM-22 family molecularsieve is ERB-1, ITQ-1, ITQ-2, ITQ-30, PSH-3, SSZ-25, MCM-22, MCM-36,MCM-49, MCM-56, or any combination thereof.
 6. The process of claim 2,wherein said second molecular sieve comprises a molecular sieve selectedfrom a group consisting of zeolite beta, zeolite Y, Ultrastable Y,Dealuminized Y, rare earth exchanged Y, mordenite, TEA-mordenite,silicalite, ZSM-3, ZSM-4, ZSM-5, ZSM-11, ZSM-12, ZSM-14, ZSM-18, ZSM-20,ZSM-22, ZSM-23, ZSM-35, and ZSM-48.
 7. The process of claim 1, whereinsaid suitable alkylation or transalkylation conditions include atemperature from about 100° C. to about 400° C., a pressure from about20.3 to 4500 kPa-a, a WHSV from about 0.1 to about 10 hr⁻¹, and a molarratio of said alkylatable compound over said alkylating agent from about0.1:1 to 50:1.
 8. The process of claim 1, wherein said monoalkylatedaromatic compound comprises ethylbenzene, said alkylatable aromaticcompound comprises benzene, and said alkylating agent comprisesethylene.
 9. The process of claim 1, wherein said monoalkylated aromaticcompound comprises cumene, said alkylatable aromatic compound comprisesbenzene, and said alkylating agent comprises propylene.
 10. The processof claim 1, wherein said condea alumina has a density in the range of500-800 g/l.
 11. The process of claim 2, wherein said second molecularsieve has a framework type of at least one of FAU, *BEA, MFI, MTW, andany combination thereof.
 12. The process of claim 1, wherein saidcatalyst composition having at least 50 wt % of said crystalline MCM-22family molecular sieve based on the total weight of said catalystcomposition.